Synthesis of alkyl t-alkyl ether

Abstract: An improved process for preparing alkyl tertiary alkyl ethers, especially methyl t-butyl ether, in one step comprises reacting tertiary alcohol and primary alcohol in the presence of a catalyst comprising β-zeolite modified with one or more metals selected from Group VIII of the Periodic Table. Optionally, the catalyst may be further modified with a halogen or a Group IB metal. The catalyst is preferably used in the presence of Group III oxide binder and, typically the reaction is carried out at a temperature of about 20°C to 250°C under a pressure from 0.1 to 7 MPa. In reaction between tertiary butanol and methanol, when the temperature is in the operating range above about 140°C, the product comprises a two-phase mix of an MTBE-isobutylene and, optionally, diisobutylene product-rich phase and a heavier aqueous ethanol-rich phase.

Description: This invention concerns an improved process for preparing alkyl tertiary alkyl ethers and particularly methyl tertiary butyl ether (MTBE) in one step by the reaction of tertiary butanol and methanol in the presence of a catalyst comprising a Beta (β) zeolite modified with one or more metals selected from Group VIII of the Periodic Table, as defined in the Condensed Chemical Dictionary, page 789 and further modified with a halogen selected from the group consisting of fluorine, chlorine, bromine and iodine. Particularly good etherification activity has been observed using platinum or palladium. The novel catalysts may optionally be further treated with a Group IB metal. The invention is especially advantageous in that the platinum/palladium-modified zeolites exhibit both high activity during methyl t-butyl ether synthesis from methanol plus t-butanol, as well as ethyl t-butyl ether synthesis from ethanol plus t-butanol. Additionally, they allow for the co-synthesis of isobutylene and diisobutylene. It is well-known that there is pressure to eliminate lead compounds from automotive fuels for reasons of public health and environmental protection. Although the specifications for reformulated gasolines set by EPA will come into force in 1995, standards were brought into force in the United States on November 1, 1992 requiring gasoline to contain 2.7 wt% oxygen during the winter in nonattainment areas of the U.S. If the federal air quality standard for CO has not been achieved by a specified attainment date, the minimum oxygen content will be increased to 3.1%. Moreover, with effect from the summer of 1992, the maximum blending Reid vapour pressure (BRvp) of all gasolines was set at 9.0 psi (0.06 MPa). Since oxygenates are not only used as gasoline blending components, extenders, octane boosters and as key ingredients for reducing the emissions of CO and VOCs (Volatile Organic Compounds), it is expected that the demand for oxygenates will increase enormously in the coming years. Of all oxygenates, the tertiary ethers, such as methyl t-butyl ether (MTBE), ethyl tert-butyl ether (ETBE), and tert-amyl methyl ether (TAME) are preferred by refineries to lighter alcohols. They have lower blending Reid vapour pressure (BRvp), lower vaporization latent heats and low solubilities in water. The most common ether in use today is MTBE with a production of about 25 million metric tons. However, ETBE is becoming more attractive as the price of methanol goes up in relation to gasoline. It can be produced from renewable ethanol, in contrast to methanol derived from natural gas, and its use would help mitigate the greenhouse effect. At the present time, TAME, which is usually produced in MTBE refinery units when C 5 olefins are diverted into the feed, is not viewed as rivalling MTBE or ETBE. The main drawback of tertiary ethers, is that they substantially increase aldehyde emissions. It is believed this could be largely circumvented by mixing the tertiary ethers with tertiary alcohols. Tertiary butyl alcohol (tBA) has a very low atmospheric reactivity and low aldehyde emissions, since no hydrogens are contained in the carbon link to the oxygen. Generally, it is known that asymmetrical C 4 -C 7 alkyl tertiary alkyl ethers are particularly useful as octane improvers for liquid fuels, especially gasoline. Methyl tertiary butyl ether (MTBE), ethyl t-butyl ether (ETBE), isopropyl t-butyl ether (IPTBE) and tertiary amyl methyl ether (TAME) are known to exhibit high octane properties. Much attention has been focused on production of these ethers due to the rapidly increasing demand for lead-free octane boosters for gasoline. It is known in the art to produce MTBE or ETBE by reacting isobutylene with either methanol or ethanol, resulting in the formation of MTBE or ETBE, respectively. The reaction is normally conducted in liquid phase with relatively mild conditions. The isobutylene can be obtained from various sources, such as naphtha cracking, catalytic cracking, etc. The resulting reaction product stream contains the desired MTBE or ETBE, as well as unreacted isobutene and other C 4 hydrocarbons and methanol or ethanol. References in the art which use tertiary butanol as a reactant and disclose MTBE or ETBE as a product usually require two stages rather than one. European patent application nos. 0 595 567 and 0 624 564, cited under Article 54(3) and (4) EPC, disclose processes for preparing alkyl tertiary-alkyl ether from tertiary alcohol and primary alcohol in the presence of a catalyst selected from β-zeolite and a β-zeolite modified with multiple metals. United States Patent 4,789,656 discloses a process for preparing a binder-free β-zeolite catalyst incorporating a highly-dispersed noble metal such as platinum. United States Patent 5,228,979 relates to a process for hydro- cracking various types of hydrocarbon feed stocks in an ammonia rich environment. The process uses a catalyst comprising a β-zeolite and a noble metal hydrogenation component, for example palladium. International patent application WO 91/00851 discloses a process and a catalyst for isomerising normal and slightly branched C 4 to C 7 hydrocarbons. The catalyst is a β-zeolite, preferably modified with one or more metals from Group XIII of the Periodic Table. In Chemical Abstracts, Vol. 119, No. 22, dated 29 November 1993, abstract no. 229886s discloses a catalytic reforming method for hydrocarbon oil using a catalyst comprising a mixed support of β-zeolite and inorganic oxide such as γ-alumina loaded with platinum, rhenium (or tin) and chlorine. European patent application no. 0 333 078 discloses a method for reacting tertiary butanol with methanol in the presence of a catalyst to provide methyl tertiary butyl ether. The catalyst is selected from the group consisting of acidic aluminas, acidic silicas, or combinations thereof with zeolites containing alumina or silica, and acidic clay mineral catalysts. European patent application no. 0 546 695 describes a method for producing alkyl tertiary alkyl ethers from primary alcohols and tertiary alcohols using a multimetal-modified faujasite zeolite catalyst. European patent application no. 0 595 567 describes a method for producing alkyl tertiary alkyl ethers from primary alcohols and tertiary alcohols using a β-zeolite catalyst or a β-zeolite catalyst modified with one or more metals selected from Groups IB, VB, VIB, VIIB, or VIII of the Periodic Table. European patent application no. 0 624 564 describes a method for producing ethyl tertiary butyl ether from t-butanol in the presence of a β-zeolite catalyst or a β-zeolite modified with multimetals selected from the group consisting of Groups IB, VB, VIB, VIIB, or VIII of the Periodic Table at a temperature of 20°C to 250°C and 0.1 to 7.0 MPa pressure. It would be a valuable advance in the art if a method were available for the synthesis of methyl and ethyl tertiary butyl ether from tertiary butanol employing one step technology and a catalyst exhibiting product phase separation at operating temperatures of 140°C or higher. The co-synthesis of isobutylene and diisobutylene using the crude feedstock reactants would make such a process even more attractive. The invention is a method of preparing alkyl tert-alkyl ether from tertiary alkyl alcohol and a C 1 -C 6 primary alcohol in one step, comprising reacting at an elevated temperature and moderate pressure a C 4 -C 10 tertiary alkyl alcohol and a C 1 -C 6 primary alcohol in the presence of a catalyst comprising a β-zeolite modified with one or more metals selected from Group VIII of the periodic Table, wherein the modified β-zeolite is optionally further treated with a Group IB metal, and continuously contacting the C 1 -C 6 primary alcohol with said C 4 -C 10 tertiary alcohol in molar proportions from 10:1 to 1:10 over said zeolite catalyst at a temperature of 20° to 250°C and a pressure of 0.1 to 7 MPa to obtain the desired alkyl tertiary-alkyl ether product, wherein the Group VIII metal-modified β-zeolite is reduced in a stream of hydrogen in the temperature range of 100° to 600°C, characterised in that: the Group VIII-modified β-zeolite is further modified with a halogen selected from the group consisting of fluorine, chlorine, bromine and iodine. The process may be applied to the reaction of a C 1 -C 6 primary alcohol such as methanol, ethanol, n-propanol or n-hexanol with a C 4 -C 10 tertiary alcohol such as, tertiary butanol or tertiary amyl alcohol. Alternatively, a mixture of alcohols, e.g., a mixture of C 1 -C 5 alcohols, could be reacted to give a mixture of alkyl tert-alkyl ethers. Methyl t-butyl ether (MTBE) and ethyl t-butyl ether (ETBE) are typical of the materials which may be prepared by the inventive process. Such preparation involves reacting tertiary butyl alcohol with methanol or ethanol in the presence of an etherification catalyst. The etherification is carried out in a single step and the catalyst comprises a β-zeolite modified with one or more metals selected from Group VIII of the Periodic Table and further modified with halogen. In a variation of the above, the β-zeolite can be further modified with copper. The reaction can be represented by the following: Generally, the methanol or ethanol and t-butanol co-reactants may be mixed in any proportion in order to generate the desired methyl t-butyl ether (MTBE) or ethyl t-butyl ether (ETBE). Preferably, however, the molar ratio of primary alcohol to t-butanol (tBA) in the feed mixture should be between 10:1 and 1:10, if the yield of desired MTBE or ETBE is to be maximized. In order to achieve maximum selectivity to MTBE or ETBE and optimum conversion per pass, an excess of primary alcohol in the liquid feed is desirable. The most preferred methanol or ethanol-to-tertiary butanol molar ratio is from 1:1 to 5:1. In certain circumstances, it may be particularly desirable that the tBA conversion is sufficiently high (e.g. 70% or greater), that the crude product mix phase separates into an isobutylene-MTBE product-rich phase and a heavier aqueous alcohol phase. Optionally, the MTBE-isobutylene phase will also contain diisobutylene. Preferably such a product phase separation would be achieved at as low an etherification temperature as possible, but it is particularly observed in the range 140°-200°C. The synthesis of Eq. 1 can also be conducted where the t-butanol and methanol reactants are mixed with certain other components including water, ketones such as acetone (Ac 2 O) and methyl ethyl ketone (MEK), peroxides and hydroperoxides such as di-t-butyl peroxide (DTBP) and allyl t-butyl peroxide (ATBP), and t-butyl hydroperoxide (TBHP), as well as esters such as t-butyl formate (TBF). Typically, each of said classes of components makes up less than 10% of the total feed mixture. As indicated above, the one-step process according to the present invention may be used for the preparation of a variety of alkyl tertiary alkyl ethers, besides MTBE and ETBE. In addition, the catalyst of the present invention could be employed as a trifunctional catalyst for the removal in the presence of hydrogen of diolefins and peroxides that are present in the C 4 or C 5 iso-olefin stream in the MTBE/TAME unit. In the modified catalyst of the present invention, good results were realized using certain crystalline aluminosilicate zeolites as catalysts for the reaction represented in Eq. 1. Particularly effective were the isostructural group of β-zeolites. The preferred forms of β-zeolite are the highly acidic, high silica forms, having silica-to-alumina mole ratio of at least 10:1, and preferably in the range of 10:1 to 50:1 in the as-synthesized form. A narrower range of 20:1 to 30:1 is most preferred. It has been found, in fact, that β-zeolite may be prepared with silica-to-alumina mole ratios above the 200:1 maximum specified in U.S. Patent No. 3,308,069 and these forms of the zeolite may perform well in the process. Ratios of 50:1, or even higher, may be used where available. Illustrative of suitable β-zeolites for the practice of this invention include Valfor C806β, Valfor CP815β and Valfor C861. Valfor® is the registered trademark of the PQ Corporation. Valfor® C806β zeolite is β-zeolite powder in template cation form. It is a high silica shape selective zeolite which contains the organic template used in the crystallization step, having been isolated after filtration and washing of the synthesis product. C806β has a SiO 2 /Al 2 O 3 molar ratio of 23-26; the crystal size is 0.1-0.7 um; the surface area after calcination is about 700-750 m 2 /g; the cyclohexane adsorption capacity after calcination is 19-24g/100g; Na 2 O content is about 0.01-1.0% by weight anhydrous; and, the organic content is about 11-13% by weight, on a water-free basis. Valfor® C815β zeolite is a calcined β-zeolite powder in hydrogen, sodium form. It is similar to C806β except the product has been calcined to decompose the organic template. C815β is a high silica, shape selective aluminosilicate with a large pore diameter. C815β also has a SiO 2 /Al 2 O 3 molar ratio of about 23-26; the crystal size, surface area, cyclohexane adsorption capacity and Na 2 O are all within the same ranges as given for C806β. Valfor® C861β is an extrudate made of 80% C815β powder and 20% alumina powder. The metals useful for modifying the zeolite in the present invention comprise those from Group VIII of the Periodic Table including, iron, ruthenium, cobalt, rhodium, nickel, palladium and platinum. Preferred metals are platinum and palladium. Especially good results were observed using a β-zeolite treated with ammonium hexafluorosilicate and subsequently treated with palladium. Said zeolites are preferably impregnated with said specified metals as their salts, particularly their metal nitrate or chloride salts, in an aqueous, alcoholic, or ketonic media over a period of 1-24 hours, then the solids are filtered off, dried at elevated temperature, e.g. 120°C, for a period of time and calcined at 300-800°C for a further period, e.g. 530°C for 5 hours followed by reduction in a stream of hydrogen at 100°-600°C. The palladium-containing precursor compound to be dispersed into the β-zeolite is prepared by first dissolving or slurring the selected palladium salt, halide, etc., e.g., palladium(II) salt, with a suitable solvent system and subsequently impregnating the β-zeolite with the palladium-containing mixture. These solutions or slurries may be poured onto the zeolite, or the zeolite may be immersed in an excess of the liquid solution or slurries, with the excess being subsequently removed. The palladium-containing precursor compound to be dispersed upon the zeolite may be impregnated on said zeolite in the form of a bivalent palladium-containing salt, such as, for example, palladium acetate, palladium propionate, palladium acetylactonate, palladium nitrate and the like. Alternatively, it can be added in the form of a palladium halide, such as palladium chloride. The examples demonstrate the use of tetraminepalladium(II) nitrate, Pd(NH 3 ) 4 (NO 3 ) 2 . Where the β-zeolite is modified with platinum, it is preferably in the form of a nitrate or halide. Various possible platinum catalysts would include PtCl 2 , PtBr 2 , (PhCN) 2 PtCl 2 , (Ph 3 P) 2 PtCl 2 , Pt(acac) 2 or tetraamineplatinum(II) nitrate, Pt(NH 3 ) 4 (NO 3 ) 2 . Particularly effective in the subject synthesis of ETBE or MTBE are the palladium/platinum-modified β-zeolites modified with a halogen compound and further modified with a Group IB compound, particularly copper and silver compounds. Halogens which may be employed include fluoride, chloride, bromide and iodide compounds. Fluoride-containing compounds are preferred. Good results were observed using ammonium hexafluorosilicate. The copper-containing compound is added to the zeolite in the form of a salt of copper such as halide, sulphate, trifluoroacetate, nitrate, naphthalenate, hex-3-endioates or acetate. Copper salts which work include, but are not limited to copper(II) chloride, copper(II) bromide, copper(II) sulphate, cuprous chloride hydrate, copper(II) trifluoroacetate, copper(II) acetate, copper(II) triflate, copper(II) fluorosulfonate, copper(I) chloride and copper(I) sulphate. The amount of the various metals impregnated into the zeolite can vary. The amount of each individual metal, i.e., palladium, platinum, fluorine and copper can vary from 0.01 to 10.0%. Where palladium and platinum are deposited on β-zeolite the preferred weight percent is from 0.1% to 1.0%. Example 1 demonstrates the preparation of the modified catalysts. Salts containing fluorine and palladium in anhydrous or hydrated forms were dissolved in water, alcohol, or acetone and the β-zeolites were added. The catalysts were then calcined by heating to 300° to 800°C and reduced in a stream of hydrogen at 100° to 600°C. Said catalysts may be in the form of powders, pellets, granules, spheres, shapes and extrudates. The examples described herein demonstrate the advantages of using extrudates. The reaction may be carried out in either a stirred, slurry reactor or in a fixed bed continuous flow reactor. The catalyst concentration should be sufficient to provide the desired catalytic effect. Said catalysts may be formed in the presence of a binder, such as Group III or Group IV oxide. Group III or IV oxides used in conjunction with said palladium/platinum-modified β-zeolite include oxides of aluminum, silicon, titanium, zirconium, hafnium, germanium, tin and lead, as well as combinations thereof. Alumina is preferred. Said binders may comprise 10% to 90% of the formed catalyst. Etherification can generally be conducted at temperatures from 20° to 250°C; the preferred range being 80° to 200°C. Good results are observed throughout this temperature range. The total operating pressure may be from 0 to 1000 psig (0.1 to 7 MPa), or higher. The preferred pressure range is 50 to 500 psig (0.35 to 3.5 MPa). Typically, MTBE is generated continuously in up to ca. 40 wt% concentration or greater in the crude liquid product at total liquid hourly space velocities (LHSV) of up to 6 or higher and relatively mild conditions, where: LHSV = Volume Of Total Liquid Feed Run Through The Reactor Per Hour Volume of Catalyst In Reactor Conversions of t-butanol (tBA, wt%) are estimated in the following examples using the equation given below: (Mole% of tBA in Feed - Mole% of tBA in Product) Mole% of tBA in Feed x 100 The examples which follow illustrate the one-step synthesis of MTBE from tBA and MeOH (Eq. 1) using palladium/platinum-modified β-zeolites particularly in the form of extrudates. Ethyl t-butyl ether (ETBE) synthesis has also been confirmed. In particular, the accompanying examples illustrate: 1) The co-synthesis of MTBE, isobutylene, diisobutylene in Example 3 from t-butanol/methanol via etherification, dehydration and dimerization reactions using a palladium, fluoride-modified β-zeolite catalyst, prepared by the method of Example 1. Here the tBA conversion levels vary from 69% to 96% per pass over the operating temperature range 120°-180°C. Product phase separation into a lighter, diisobutylene, isobutylene, MTBE product phase and a heavier aqueous methanol phase is achieved at temperatures from 140°C and above. A wide range of MTBE, isobutylene and diisobutylene selectivities have been demonstrated in this experiment. 2) In Examples 4-7, the co-synthesis of MTBE, isobutylene and diisobutylene from MeOH/tBuOH are illustrated using: a. A palladium, copper-modified β-zeolite. b. A platinum-modified β-zeolite. c. A palladium, fluoride-modified β-zeolite with 70% alumina binder. 3) In Example 8, ethyl t-butyl ether synthesis from ethanol and t-butanol is demonstrated using the palladium, fluoride-modified β-zeolite catalyst of Example 1. EXAMPLE 1 This example illustrates the preparation of a palladium-modified β-zeolite. To 110g of β-zeolite (090-92-1027-700, 50% β-zeolite, 50% alumina calcined at 530°C for 3 hours) in 1/16" (1.6 mm) diameter extruded form was added a solution of 1.72g of ammonium hexafluorosilicate in 84 ml of distilled water. Impregnation of the β-zeolite was allowed to proceed over 1-2 hours, then the solids were filtered off, dried at 120°C, and calcined at 530°C for 2 hours. The fluorosilicate-treated zeolite was next mixed with a solution of 0.69g of tetraaminepalladium(II) nitrate, Pd(NH 3 ) 4 (NO 3 ) 2 , in 90 ml of distilled water, the solids recovered by filtration and then dried at 120°C overnight, calcined at 530°C for 5 hours, and finally reduced in a stream of hydrogen at 200°C. The grey-coloured extrudates (052-92-6887-021) were found by analysis to contain: 0.24% fluoride 0.2% palladium EXAMPLE 2 (Comparative) This example illustrates the preparation of a platinum-modified β-zeolite. To 176g of β-zeolite (090-92-1027-700, 50% β-zeolite, 50% alumina) in 1/16" (1.6 mm) diameter extruded form was added a solution of 1.75g of tetraamineplatinum(II) nitrate, Pt(NH 3 ) 4 (NO 3 ) 2 , in 120 ml of distilled water. Impregnation of the β-zeolite was allowed to proceed over 1-2 hours, then the solids were filtered off, dried at 120°C for 2 hours, calcined at 530°C for 3 hours and finally reduced at 400°C in a stream of hydrogen for 4 hours. The brown-black extrudates (052-92-6887-047) were found by analysis to contain: 0.22% platinum EXAMPLE 3 This example illustrates the production of methyl t-butyl ether from t-butanol and methanol using the palladium-impregnated β-zeolite of Example 1. Synthesis was conducted in a tubular reactor (12.5 mm i.d., 300 mm long) constructed of 316 stainless steel, operated upflow and mounted in a furnace, controllable to ±1.0°C and fitted with pumps allowing flow control to <±1 cc/hr. The reactor was also fitted with a pressure regulating device and equipment for monitoring temperature, pressure and flow rate. The reactor was charged at the beginning of the experiment with 25 of palladium-treated β-zeolite, prepared by the procedure of Example 1, as 1/16" (1.6 mm) diameter extrudates. A screen of glass wool was placed at the top and bottom of the reactor to ensure the catalyst would remain in the middle portion. The catalyst bed was treated with a methanol/t-butanol (1.1:1 molar mix) upflow, at a rate of 50 cc/hr, while the reactor was held at 120°C, under a total pressure of 300 psi (2.1 MPa). Samples of crude product effluent were collected periodically on stream, in 316 ss bombs and analyzed by glc. Typical analyses data for samples taken under these conditions are summarized in Table 1. Concentrations of MTBE, isobutylene, diisobutylene, methanol, t-butanol in the product effluent were also measured at a series of higher temperatures (140°-180°C). These data are also included in Table 1. For Sample #2, at 120°C: tBA conversion = 69% MTBE selectivity = 73% Isobutylene selectivity = 20% Diisobutylene selectivity = 5% For Sample #7, at 180°C: tBA conversion = 96% MTBE selectivity = 12% Isobutylene selectivity = 71% Diisobutylene selectivity = 20% EXAMPLES 4-7 Using the equipment and following the procedures of Example 3, various platinum and palladium-impregnated β-zeolite catalysts were treated with a 1.1:1 molar mix of methanol and t-butanol at a series of temperatures from 120° to 160°C. Concentrations of MTBE, isobutylene, diisobutylene, methanol and t-butanol in the product effluents, under the specified condition, as determined by glc, are summarized for each catalyst in the accompanying Tables 2 to 5. The catalysts evaluated include: a) A 1% F, 0.3% Pd on 50% β-zeolite, 50% alumina, reduced at 200°C (Sample 052-92-6887-219, Example 4, Table 2). b) A 0.2% Pd, 2% Cu on 50% β-zeolite, 50% alumina, reduced at 200°C (Sample 052-92-6887-128, Example 5, Table 3). c) A 0.2% Pt on 50% β-zeolite, 50% alumina, reduced at 400°C and prepared by the procedures of Example 2 (Sample 052-92-6887-047, Example 6, Table 4). d) A 1% F, 0.3% Pd on 30% β-zeolite, 70% alumina (Sample 052-92-6887-119, Example 7, Table 5). All four modified β-zeolites give high yields of MTBE at the lower operating temperatures (e.g. 120°C) and high yields of isobutylene at the higher temperatures (e.g. 160°C). Of note, for the platinum-modified β-zeolite of Example 6: At 120°C: tBA conversion = 72% MTBE selectivity = 68% Isobutylene selectivity = 19% Diisobutylene selectivity = 9% At 160°C: tBA conversion = 92% EXAMPLE 8 Using the equipment and following the procedure of Example 3, the palladium, fluoride-modified β-zeolite of Example 1 was treated with a 1.1:1 molar mix of ethanol and t-butanol at a series of temperatures from 120°C to 160°C. Concentrations of ethyl t-butyl ether (ETBE), isobutylene, diisobutylene, ethanol and t-butanol in the product effluents, under the specified conditions, as determined by glc, are summarized in the accompanying Table 6.

Claims: A method of preparing alkyl tert-alkyl ether from tertiary alkyl alcohol and a C 1 -C 6 primary alcohol in one step, comprising reacting at an elevated temperature and moderate pressure a C 4 -C 10 tertiary alkyl alcohol and a C 1 -C 6 primary alcohol in the presence of a catalyst comprising a β-zeolite modified with one or more metals selected from Group VIII of the Periodic Table, wherein the modified β-zeolite is optionally further treated with a Group IB metal, and continuously contacting the C 1 -C 6 primary alcohol with said C 4 -C 10 tertiary alcohol in molar proportions from 10:1 to 1:10 over said zeolite catalyst at a temperature of 20° to 250°C and a pressure of 0.1 to 7 MPa to obtain the desired alkyl tertiary-alkyl ether product, wherein the Group VIII metal-modified β-zeolite is reduced in a stream of hydrogen in the temperature range of 100° to 600°C, characterised in that: the Group VIII-modified β-zeolite is further modified with a halogen selected from the group consisting of fluorine, chlorine, bromine and iodine. A method as claimed in claim 1 wherein the C 4 -C 10 tertiary alkyl alcohol is t-butanol and the C 1 -C 6 primary alcohol is methanol or ethanol. A method as claimed in claim 1 or claim 2 wherein the β-zeolite has a silica:alumina molar ratio of at least 10:1. A method as claimed in any preceding claim wherein the Group VIII metals are selected from the group consisting of iron, ruthenium, osmium, cobalt, rhodium, iridium, nickel, palladium and platinum. A method as claimed in claim 4 wherein the Group VIII metal is palladium or platinum impregnated into the β-zeolite as tetraaminepalladium(II) nitrate or tetraamineplatinum(II) nitrate, respectively. A method as claimed in any preceding claim wherein the halogen is fluorine added as ammonium hexafluorosilicate. A method as claimed in any preceding claim wherein the Group VIII- and halogen-modified β-zeolite is further modified with a metal selected from Group IB of the Periodic Table. A method as claimed in claim 7 wherein the Group IB metal is selected from the group consisting of copper and silver. A method as claimed in any preceding claim wherein the concentrations of metals impregnated into said zeolite vary from 0.01% to 10.0% for each metal. A method as claimed in any preceding claim wherein the β-zeolite catalyst is formed in the presence of a Group III oxide. A method as claimed in claim 10 wherein the Group III oxide binder is alumina. A method as claimed in any preceding claim wherein the operating temperature is in the range of 140°C to 200°C and the product comprises a two-phase mix of an ETBE-isobutylene, and, optionally, diisobutylene product rich phase and a heavier aqueous ethanol-rich phase.

Inventors: DAI PEI-SHING EUGENE, KNIFTON JOHN FREDERICK, DAI, PEI-SHING EUGENE, KNIFTON, JOHN FREDERICK
Applicants: HUNTSMAN SPEC CHEM CORP, HUNTSMAN SPECIALTY CHEMICALS CORPORATION
Application year: 1994
Main classification: C07C43
IPC codes: C07B61, B01J29, C07C43, C07C41